CN104498070A - Smoke mixed type heat carrier retorting process of oil shale - Google Patents
Smoke mixed type heat carrier retorting process of oil shale Download PDFInfo
- Publication number
- CN104498070A CN104498070A CN201410841407.7A CN201410841407A CN104498070A CN 104498070 A CN104498070 A CN 104498070A CN 201410841407 A CN201410841407 A CN 201410841407A CN 104498070 A CN104498070 A CN 104498070A
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- gas
- heat
- shale
- oil
- temperature
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/06—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of oil shale and/or or bituminous rocks
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a smoke mixed type heat carrier retorting process of oil shale. The process is characterized is that 10-75mm particular oil shale exchanges heat with the smoke at the temperature of 250 to 300 DEG C from a first-stage efficient heat pipe heat exchanger; the small particular oil shale being more than 0 to 10mm enters a circulating fluidized bed boiler to be combusted to generate smoke at the temperature of 850 to 950 DEG C; the smoke in one way supplies exchange heat to a second-stage efficient heat pipe heat exchanger, and the smoke in another way enters a medium-temperature retorting section in a retorting furnace from the retorting furnace so as to supply heat for medium-temperature retorting; the dry oil shale can generate tar-containing mixed gas to be exported from the retorting furnace to be retorted so as to obtain semi-coke, and the semi-coke is discharged from the bottom of the furnace; oil gas from an outlet of the retorting furnace is processed by a recovering system to recover the shale oil and light oil; the smoke at the temperature of 950 DEG C, produced through the semi-coke exchanges heat until reaching the temperature of 600 DEG C and then flows from a circulating gas inlet in a low-temperature retorting section at the middle part of the retorting furnace into the low-temperature retorting section of the retorting furnace, so as to be used as a heat source for retorting of the oil shale.
Description
Technical field
The present invention relates to oil shale distillation field, is the hybrid thermal barrier distillation process of a kind of resinous shale flue gas.
Background technology
Along with the day by day exhaustion of hydrocarbon resources, along with being on the rise of domestic and international hydrocarbon resources situation, resinous shale is as a kind of unconventional petroleum resources, and its product shale oil is considered as the substitution of oil, receives increasing concern and attention.Now main production oil shale distillation process is two kinds both at home and abroad: one is solid thermal carriers, another kind of gaseous heat-carrier; The deficiency of existing gaseous heat-carrier retorting technique is: 1, gaseous heat-carrier can only use the block resinous shale of about 10-75mm to carry out destructive distillation, oil yield is between 63-75%, the 0-10mm granule wax shale accounting for total resources 25% can not utilize, the overall low utilization of resources 50%; 2, Fushun formula destructive distillation heating system uses accumulation of heat batch kiln, pyrolysis temperature is caused to fluctuate, the way that gas retort uses retort section to combine with segment occurred, but have not exclusively superfluous the supporting of segment occurred reaction to alter burning oil condition, therefore formula distillation system comprehensive on average oil-collecting ratio in Fushun is about 63%; 3, loopful follows formula distillation system, because system cannot for carrying enough heats, even if additional producer gas generator heat supply, but economy pessimistic; 4, gaseous heat-carrier thermostatically heating technology, because lightweight oil does not reclaim, therefore there is serious cracking, coking when process furnace heat exchange in circulating mash gas, causes the damage of heating system device; 5, gas combustion square gas retort, because of the problem that temperature of combustion is too high, make gas retort usually coking occur, cause treatment capacity can only reach 75% of designed capacity, the average oil yield of gas retort is between 65-70%.
Summary of the invention
The object of the invention is to carry out substantial improvements and innovation to prior art, there is provided a kind of resinous shale flue gas hybrid thermal barrier distillation process, its feature is, that starts introduces in gas retort by 850-950 DEG C of heat smoke, there is provided heat as thermal barrier to gas retort, circular fluid bed, efficient heat-pipe heat-exchanger, recovering of vaporized hydrocarbons system, that flue gas closes mixing gas retort is integrated, reaches resinous shale comprehensive utilization ratio 100%, separate unit gas retort treatment capacity improves 25%, and comprehensive oil-collecting ratio reaches 90%.
The technical scheme realizing the object of the invention employing is, the hybrid thermal barrier distillation process of a kind of resinous shale flue gas, it has in comprising: oil shale ore enters in destructive distillation furnace roof storage bunker Yu from one-level efficient heat-pipe heat-exchanger temperature 250-300 DEG C of flue gas through the resinous shale that pulverizing-screening system makes 10-75mm particle carries out heat exchange, the granule wax shale of >0-10mm enters burning in circulating fluid bed boiler and produces 850-950 DEG C of flue gas, flue gas is divided into two-way, one tunnel provides heat-shift for secondary efficient heat-pipe heat-exchanger, another road enters the medium temperature carbonization section in gas retort from the medium temperature carbonization section mixing chamber inlet in gas retort, heat needed for medium temperature carbonization is provided, dry resinous shale enters in the low-temperature pyrolysis section in gas retort through feed opening, constantly move down by the continuous running of self gravitation along with ash ejector, shale in stove is constantly declined, in gas retort, operating resinous shale is subject to the constant temperature 600 DEG C of heating gas provided continuously from heating system and the 650 DEG C of gas heat supplies produced with medium temperature carbonization section, from top to down carries out depth drying, preheating and retort process, after the mixed gas generated containing tar rises, derive gas retort through central airway from gas retort gas exit, enter recovery system, resinous shale generates semicoke after twice destructive distillation, discharge out of the furnace after basin cooling from furnace bottom, stay and do its use, gas retort temperature out 120-180 DEG C of gas oil gas reclaims the shale oil of 85% through recovery system, the gas of 35-55 DEG C is at the lightweight oil reclaiming 15% through light oil recovery unit, shale oil and lightweight oil enter metering storage system respectively, after purification, the methane gas of 35-55 DEG C first carries out heat exchange by one-level efficient heat-pipe heat-exchanger and 650 DEG C of flue gases from secondary efficient heat-pipe heat-exchanger, produce the circulating mash gas of 350-450 DEG C, the flue gas of 950 DEG C produced at feeding secondary efficient heat-pipe heat-exchanger and burning in circulating fluid bed boiler small-particle semicoke carries out heat exchange to 600 DEG C, in the middle part of gas retort, low-temperature pyrolysis section circulating mash gas entrance passes in gas retort low-temperature pyrolysis section, as the thermal source of oil shale distillation.
The advantage applies of the hybrid thermal barrier distillation process of resinous shale flue gas of the present invention exists:
1, the hybrid thermal barrier distillation process of flue gas, the block resinous shale of 10-75mm enters in gas retort, and the granule wax shale of >0-10mm enters burning in circulating fluid bed boiler, realizes resource utilization 100%;
2, the hybrid thermal barrier distillation process of flue gas, the high-temperature hot flue gas of 950 DEG C of flue gases that burning in circulating fluid bed boiler produces and circulating mash gas heat exchange in hot tube high-efficiency interchanger generate the thermal circulation gas of 650 DEG C, solve the problem that recycle to extinction process system cannot meet self heat deficiency;
3, the hybrid thermal barrier distillation process of flue gas, the combination of 400 DEG C, 650 DEG C two stage hot pipe high-performance heat exchangers and lightweight recovery system, thoroughly solves heat transfer tube coking, and the problem that thermo-efficiency reduces realizes real constant temperature continuous heating system;
4, the hybrid thermal barrier distillation process of flue gas, because passing into 600-950 DEG C of flue gas as gas retort supplemental heat source, the existing gas retort of thorough solution is because superfluous oxygen alters problem, the limit of present single stove treatment capacity 100-120 ton per day can be surmounted, single stove treatment capacity 180 tons, gas retort oil yield improves 20%, reaches 95%;
5, the hybrid thermal barrier distillation process of flue gas, because passing into 600-950 DEG C of flue gas as gas retort supplemental heat source, thoroughly solve the gas side of combustion stove because of temperature of combustion too high, and produce coking problem, single stove treatment capacity 25% can be improved, distillation system oil rate improve 20%.
Accompanying drawing explanation
Fig. 1 is a kind of resinous shale flue gas of the present invention hybrid thermal barrier destructive distillation flow scheme figure.
In figure: the Wen Gan section of staying smoke inlet, 12 recovery systems, 13 light oil recovery units, 14 oil gas metering storing and transporting systems in 1 pulverizing-screening system, 2 circulating fluidized bed pots, 3 one-level efficient heat-pipe heat-exchangers, 4 secondary efficient heat-pipe heat-exchangers, 5 gas retort low-temperature pyrolysis section thermal circulation gas entrances, 6 destructive distillation furnace roof storage bunkers, 7 retort gases outlets, 8 central airway, 9 gas retort low-temperature pyrolysis sections, 10 gas retort medium temperature carbonization sections, 11 gas retorts.
Embodiment
With reference to Fig. 1, the hybrid thermal barrier distillation process of a kind of resinous shale flue gas of the present invention, have in comprising: oil shale ore makes the granule wax shale of >0-10mm and the block resinous shale of 10-75mm through tertiary crushing and twice screening, the block resinous shale of 10-75mm particle enters in destructive distillation furnace roof storage bunker 6 Yu from one-level efficient heat-pipe heat-exchanger 3 temperature 250-300 DEG C of flue gas and carries out heat exchange, resinous shale is dried to 105 DEG C, remove surface water and dust, flue gas after heat exchange is delivered to flue gas purification system and is purified, rear discharge up to standard, the granule wax shale of >0-10mm enters circular fluid bed 2 burning and produces 850-950 DEG C of flue gas, flue gas is divided into two-way, one tunnel provides heat-shift for secondary efficient heat-pipe heat-exchanger 4, another road enters the medium temperature carbonization section 10 in gas retort from the medium temperature carbonization section mixing chamber inlet 11 in gas retort, heat needed for medium temperature carbonization is provided, dry resinous shale enters in the low-temperature pyrolysis section 9 in gas retort through feed opening, constantly move down by the continuous running of self gravitation along with ash ejector, shale in stove is constantly declined, in gas retort, operating resinous shale is subject to the constant temperature 600 DEG C of heating gas provided continuously from heating system and the 650 DEG C of gas heat supplies produced with medium temperature carbonization section 10, from top to down carries out depth drying, preheating and retort process, after the mixed gas generated containing tar rises, derive gas retort through central airway 8 from gas retort gas exit 7, enter recovery system 12, resinous shale generates semicoke after twice destructive distillation, discharge out of the furnace after basin cooling from furnace bottom, stay and do its use, gas retort temperature out 120-180 DEG C of gas oil gas is through the equipment such as cyclonic separator, indirect cool tower, electrical tar precipitator of recovery system 12, reclaim the shale oil of 85%, and make oil-containing coal mine gas be reduced to 35-55 DEG C, oil-containing coal mine gas is at the lightweight oil reclaiming 15% through light oil recovery unit 13, shale oil and lightweight oil enter respectively and measure storage system 14, carry out respectively measuring and store and transport, the clean coal mine gas that purification is latter 35-40 DEG C, send into one-level efficient heat-pipe heat-exchanger 3 and carry out heat exchange with 650 DEG C of flue gases from secondary efficient heat-pipe heat-exchanger 4, produce the circulating mash gas of 350-400 DEG C, carry out heat exchange to 600 DEG C sending into secondary efficient heat-pipe heat-exchanger 4 and circular fluid bed 2 flue gas of 950 DEG C that small-particle semicoke produces that burns, in the middle part of gas retort, low-temperature pyrolysis section circulating mash gas entrance 5 passes in gas retort low-temperature pyrolysis section, as the thermal source of oil shale distillation.
Claims (1)
1. the hybrid thermal barrier distillation process of resinous shale flue gas, it has in comprising: oil shale ore enters in destructive distillation furnace roof storage bunker Yu from one-level efficient heat-pipe heat-exchanger temperature 250-300 DEG C of flue gas through the resinous shale that pulverizing-screening system makes 10-75mm particle carries out heat exchange, the granule wax shale of >0-10mm enters burning in circulating fluid bed boiler and produces 850-950 DEG C of flue gas, flue gas is divided into two-way, one tunnel provides heat-shift for secondary efficient heat-pipe heat-exchanger, another road enters the medium temperature carbonization section in gas retort from the medium temperature carbonization section mixing chamber inlet in gas retort, heat needed for medium temperature carbonization is provided, dry resinous shale enters in the low-temperature pyrolysis section in gas retort through feed opening, constantly move down by the continuous running of self gravitation along with ash ejector, shale in stove is constantly declined, in gas retort, operating resinous shale is subject to the constant temperature 600 DEG C of heating gas provided continuously from heating system and the 650 DEG C of gas heat supplies produced with medium temperature carbonization section, from top to down carries out depth drying, preheating and retort process, after the mixed gas generated containing tar rises, derive gas retort through central airway from gas retort gas exit, enter recovery system, resinous shale generates semicoke after twice destructive distillation, discharge out of the furnace after basin cooling from furnace bottom, stay and do its use, gas retort temperature out 120-180 DEG C of gas oil gas reclaims the shale oil of 85% through recovery system, the gas of 35-55 DEG C is at the lightweight oil reclaiming 15% through light oil recovery unit, shale oil and lightweight oil enter metering storage system respectively, after purification, the methane gas of 35-40 DEG C first carries out heat exchange by one-level efficient heat-pipe heat-exchanger and 650 DEG C of flue gases from secondary efficient heat-pipe heat-exchanger, produce the circulating mash gas of 350-450 DEG C, the flue gas of 950 DEG C produced at feeding secondary efficient heat-pipe heat-exchanger and burning in circulating fluid bed boiler small-particle semicoke carries out heat exchange to 600 DEG C, in the middle part of gas retort, low-temperature pyrolysis section circulating mash gas entrance passes in gas retort low-temperature pyrolysis section, as the thermal source of oil shale distillation.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410841407.7A CN104498070B (en) | 2014-12-30 | 2014-12-30 | Smoke mixed type heat carrier retorting process of oil shale |
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| CN201410841407.7A CN104498070B (en) | 2014-12-30 | 2014-12-30 | Smoke mixed type heat carrier retorting process of oil shale |
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| CN104498070A true CN104498070A (en) | 2015-04-08 |
| CN104498070B CN104498070B (en) | 2017-01-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2687411C1 (en) * | 2018-10-31 | 2019-05-13 | Общество с ограниченной ответственностью "Сибнииуглеобогащение" | Method of producing medium-temperature coke |
| CN110172359A (en) * | 2019-05-31 | 2019-08-27 | 北京龙源宏达科技发展有限公司 | Combined type gas retort |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2232444Y (en) * | 1995-10-10 | 1996-08-07 | 季可达 | Upright dry distillation furnace body with low-temp., medium temp. and high-temp. continuous dry distillation for coal |
| CN102911682A (en) * | 2011-08-03 | 2013-02-06 | 张�诚 | Coke heat-carrying coal cracking device using moving bed with multiple feed openings as reactor |
| CN103205267A (en) * | 2013-04-18 | 2013-07-17 | 陕西煤业化工技术研究院有限责任公司 | Medium and low temperature distillation furnace of coal, distillation device based on distillation furnace, and distillation method |
-
2014
- 2014-12-30 CN CN201410841407.7A patent/CN104498070B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2232444Y (en) * | 1995-10-10 | 1996-08-07 | 季可达 | Upright dry distillation furnace body with low-temp., medium temp. and high-temp. continuous dry distillation for coal |
| CN102911682A (en) * | 2011-08-03 | 2013-02-06 | 张�诚 | Coke heat-carrying coal cracking device using moving bed with multiple feed openings as reactor |
| CN103205267A (en) * | 2013-04-18 | 2013-07-17 | 陕西煤业化工技术研究院有限责任公司 | Medium and low temperature distillation furnace of coal, distillation device based on distillation furnace, and distillation method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2687411C1 (en) * | 2018-10-31 | 2019-05-13 | Общество с ограниченной ответственностью "Сибнииуглеобогащение" | Method of producing medium-temperature coke |
| CN110172359A (en) * | 2019-05-31 | 2019-08-27 | 北京龙源宏达科技发展有限公司 | Combined type gas retort |
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| CN104498070B (en) | 2017-01-18 |
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